{"id":160,"date":"2017-03-01T15:10:23","date_gmt":"2017-03-01T15:10:23","guid":{"rendered":"http:\/\/www.fledged.eu\/?page_id=160"},"modified":"2020-09-24T10:20:19","modified_gmt":"2020-09-24T10:20:19","slug":"newsletter","status":"publish","type":"page","link":"https:\/\/www.fledged.eu\/download\/newsletter\/","title":{"rendered":"Newsletter"},"content":{"rendered":"<h2 class=\"wp-block-heading\"> <br><a aria-label=\"undefined (opens in a new tab)\" rel=\"noreferrer noopener\" href=\"\/wp-content\/uploads\/Downloads\/Newsletter\/FLEDGED%20-%20Newsletter%20-%2005%20-%20Jun2020.pdf\" target=\"_blank\">Newsletter #6 &#8211; September 2020<\/a> <\/h2>\n\n\n\n<p>Download pdf version <a href=\"\/wp-content\/uploads\/Downloads\/Newsletter\/FLEDGED%20-%20Newsletter%20-%2006%20-%20Sept2020.pdf\" target=\"_blank\" rel=\"noreferrer noopener\">here<\/a>. Previous newsletters: <a href=\"\/?page_id=1168\">Newsletter #1<\/a>, <a href=\"\/?page_id=1399\">Newsletter #2<\/a>,  <a href=\"\/?page_id=1560\">Newsletter #3<\/a>, <a href=\"https:\/\/www.fledged.eu\/?page_id=1742\">Newsletter #4<\/a>, <a href=\"https:\/\/www.fledged.eu\/?page_id=1831\">Newsletter #5<\/a><\/p>\n\n\n<div style=\"display:block\">\n<!-- FlowPaper PDF flipbook plugin v.2.0.6 wordpress.org\/plugins\/flowpaper\/ -->\n<iframe title=\"FlowPaper flipbook pdf viewer\" width=\"100%\" height=\"500\" scrolling=\"no\" class=\"flowpaper-class\" frameborder=\"0\" allowFullScreen=\"true\" lightbox=\"false\" cover id src = \"https:\/\/flowpaper.com\/flipbook\/?pdf=https:\/\/www.fledged.eu\/wp-content\/uploads\/Downloads\/Newsletter\/FLEDGED%20-%20Newsletter%20-%2006%20-%20Sept2020.pdf?wp-hosted=1&title=&header=&theme=&singlepage=&thumbs=1&modified=2009241020\" seamless=\"seamless\" style=\"margin-bottom:0;display:block;\">Your browser does not seem to support iframes. <a href=\"https:\/\/flowpaper.com\/flipbook\/?pdf=https:\/\/www.fledged.eu\/wp-content\/uploads\/Downloads\/Newsletter\/FLEDGED%20-%20Newsletter%20-%2006%20-%20Sept2020.pdf?wp-hosted=1\" target=\"_blank\">Click here to read this PDF<\/a>.<\/iframe>\n<div id=\"flowpaper-logo-bottom\" class=\"flowpaper-logo-bg\" style=\"background:linear-gradient(to right, rgba(0,0,0,0.65) 0%,rgba(0,0,0,0) 200px);width:100%;height:19px; padding-bottom: 1px; padding-left: 5px; padding-right: 10px; display: flex; align-items: center;z-index:9999\"><span style=\"height: 37px; padding-left: 6px;width:90%\"> <a id=\"flowpaper-link\" style=\"fill: #fff\" alt=\"FlowPaper logotype\" title=\"FlowPaper logotype\" href=\"https:\/\/flowpaper.com\" target=\"_blank\"> <img decoding=\"async\" alt=\"Publish PDF flipbooks online\" style=\"height:17px;width:auto;margin-top:11px;\" src=\"https:\/\/www.fledged.eu\/wp-content\/plugins\/flowpaper-lite-pdf-flipbook\/assets\/flowpaper-logo.png\" border=\"0\"> <\/a> <\/span><span style=\" float: right; right: 0; font-size: 10px; white-space: nowrap; opacity:0.8\"><a href=\"https:\/\/flowpaper.com\/flipbook-maker\/\" target=\"_new\" style=\"text-decoration:none;border-bottom:none;\">Created using FlowPaper Flipbook Maker &#8599;<\/a><\/span><\/div><\/div>\r\n                <script>\r\n                document.addEventListener(\"DOMContentLoaded\", function(){\r\n                    var target_element, iframe_element;\r\n                    iframe_element = document.querySelector(\"iframe.flowpaper-class\");\r\n                    target_element = document.querySelector(\"\");\r\n                    iframe_element.style.height = target_element.offsetHeight + \"px\";\r\n                });\r\n                <\/script>\r\n            \n\n\n\n<figure class=\"wp-block-image\"><img loading=\"lazy\" decoding=\"async\" width=\"1024\" height=\"345\" src=\"https:\/\/www.fledged.eu\/wp-content\/uploads\/BannerFledged-1-1024x345.png\" alt=\"\" class=\"wp-image-1025\" srcset=\"https:\/\/www.fledged.eu\/wp-content\/uploads\/BannerFledged-1-1024x345.png 1024w, https:\/\/www.fledged.eu\/wp-content\/uploads\/BannerFledged-1-300x101.png 300w, https:\/\/www.fledged.eu\/wp-content\/uploads\/BannerFledged-1-768x259.png 768w, https:\/\/www.fledged.eu\/wp-content\/uploads\/BannerFledged-1-1200x404.png 1200w, https:\/\/www.fledged.eu\/wp-content\/uploads\/BannerFledged-1-594x200.png 594w, https:\/\/www.fledged.eu\/wp-content\/uploads\/BannerFledged-1.png 1500w\" sizes=\"auto, (max-width: 1024px) 100vw, 1024px\" \/><\/figure>\n\n\n\n<h3 class=\"has-text-align-center wp-block-heading\"><strong><strong>FLEDGED activities on biomass gasification are completed and in the last months the work focused on Sorption-Enhanced DME synthesis<\/strong> \u2026<\/strong><\/h3>\n\n\n\n<ul class=\"wp-block-list\"><li>TRL5 experimental testing of the <strong>complete SEDMES operating cycle<\/strong> has been concluded at TNO, supported by\u00a0 SEDMES cycle modelling for operation mode design and optimization.<\/li><li><strong>Catalyst development<\/strong> for direct DME synthesis in presence of sorbent for Sorption-Enhanced synthesis has been performed at ICP-CSIC laboratories in Madrid.<\/li><li>A <strong>2D + 1D heterogeneous dynamic model<\/strong>of the reactor tube for design optimization has been successfully developed by POLIMI, validated and applied for defining operating parameters on thermal behavior and DME yield performances of the reactor.<\/li><\/ul>\n\n\n\n<p>More details and <strong><em>short presentations<\/em><\/strong> about all the activities of  the partners are available on the <a aria-label=\"undefined (opens in a new tab)\" rel=\"noreferrer noopener\" href=\"https:\/\/www.fledged.eu\/workshop\/\" target=\"_blank\">intermediate workshop dedicated webpage<\/a>.<\/p>\n\n\n\n<h3 class=\"wp-block-heading\"><strong>TRL 5 demonstration of Sorption-Enhanced DME Synthesis<\/strong> <strong>and modelling activities on cycle optimization (TNO)<\/strong><\/h3>\n\n\n\n<p><strong>Cycle design <\/strong>for six columns SEDMES unit with implemented pressure equalization system meets the following boundary conditions: 1)continuous feed stream; 2)continuous DME production; 3)continuous purge stream. Six step pressure swing adsorption (PSA) cycle (total 45 minutes) consists of:<\/p>\n\n\n\n<ul class=\"wp-block-list\"><li><strong>ADS<\/strong> \u00a0 adsorption step (DME production);<\/li><li><strong>PEQDN<\/strong> \u00a0 pressure equalization down (depressurisation);<\/li><li><strong>BD<\/strong> \u00a0 blowdown (depressurisation);<\/li><li><strong>PURGE<\/strong> \u00a0 purge (regeneration);\u00a0\u00a0<\/li><li><strong>PEQUP<\/strong> \u00a0 pressure equalization up (pressurization);<\/li><li><strong>REP<\/strong> \u00a0 repressurisation (pressurization).<\/li><\/ul>\n\n\n\n<div class=\"wp-block-image\"><figure class=\"aligncenter size-large is-resized\"><img loading=\"lazy\" decoding=\"async\" src=\"https:\/\/www.fledged.eu\/wp-content\/uploads\/N6_SEDMEScycle.png\" alt=\"\" class=\"wp-image-1841\" width=\"387\" height=\"458\" srcset=\"https:\/\/www.fledged.eu\/wp-content\/uploads\/N6_SEDMEScycle.png 479w, https:\/\/www.fledged.eu\/wp-content\/uploads\/N6_SEDMEScycle-253x300.png 253w\" sizes=\"auto, (max-width: 387px) 100vw, 387px\" \/><figcaption><em>Reference six step PSA cycle for SEDMES operation<\/em><\/figcaption><\/figure><\/div>\n\n\n\n<p>The data from the multiple simulations showed Pareto fronts, typical for PSA systems, for the defined key performance metrics C-DME, i.e. the single pass carbon selectivity to DME, and C-CO<sub>2<\/sub>, i.e. the selectivity towards CO<sub>2<\/sub>, and productivity, which allows to tune the process performance towards selectivity and productivity targets. In good agreement with experimental results, high carbon selectivity to DME can be obtained (over 95%). Similarly, the carbon selectivity to CO<sub>2<\/sub> can be reduced to less than 1%, simplifying the downstream separation. However, both come at a cost in terms of productivity. Maximum productivity can be obtained for carbon selectivity to DME of over 80%. The average productivity for a single SEDMES tube is 0.17 kg hr<sup>-1<\/sup>.<\/p>\n\n\n\n<figure class=\"wp-block-image size-large\"><img loading=\"lazy\" decoding=\"async\" width=\"962\" height=\"273\" src=\"https:\/\/www.fledged.eu\/wp-content\/uploads\/N6_SEDMESperformance.png\" alt=\"\" class=\"wp-image-1842\" srcset=\"https:\/\/www.fledged.eu\/wp-content\/uploads\/N6_SEDMESperformance.png 962w, https:\/\/www.fledged.eu\/wp-content\/uploads\/N6_SEDMESperformance-300x85.png 300w, https:\/\/www.fledged.eu\/wp-content\/uploads\/N6_SEDMESperformance-768x218.png 768w, https:\/\/www.fledged.eu\/wp-content\/uploads\/N6_SEDMESperformance-594x169.png 594w\" sizes=\"auto, (max-width: 962px) 100vw, 962px\" \/><figcaption><em>Pareto fronts for SEDMES systems key performance metrics<\/em><\/figcaption><\/figure>\n\n\n\n<p>Using the developed mathematical model it is possible to predict which process happens in the single reactor and how the components are distributed within the length of the reactor. This allows to select optimal process conditions in order to achieve maximal yield and purity of the product. For experimental validation, a 6 reactors test unit was operated at the same condition as the simulations, and the composition of the product was sampled in time. Using TNO\u2019s multi-column SEDMES reactor setup, the TRL 5 validation experiments were performed in the first half of 2020. The multi-column system allows to test complete cycle designs, e.g. including pressure equalisation steps. Besides model validation experiments at different temperatures in the range of 230-250 \u00b0C, specific conditions included CO-rich and CO<sub>2<\/sub>-rich feed gas, up to a pure H<sub>2<\/sub>-CO<sub>2<\/sub> feed gas.<\/p>\n\n\n\n<div class=\"wp-block-image\"><figure class=\"aligncenter size-large\"><img loading=\"lazy\" decoding=\"async\" width=\"873\" height=\"443\" src=\"https:\/\/www.fledged.eu\/wp-content\/uploads\/N6_SEDMEScomposition.png\" alt=\"\" class=\"wp-image-1844\" srcset=\"https:\/\/www.fledged.eu\/wp-content\/uploads\/N6_SEDMEScomposition.png 873w, https:\/\/www.fledged.eu\/wp-content\/uploads\/N6_SEDMEScomposition-300x152.png 300w, https:\/\/www.fledged.eu\/wp-content\/uploads\/N6_SEDMEScomposition-768x390.png 768w, https:\/\/www.fledged.eu\/wp-content\/uploads\/N6_SEDMEScomposition-594x301.png 594w\" sizes=\"auto, (max-width: 873px) 100vw, 873px\" \/><figcaption><em>Concentration of the gas components after each step of the cycle: purple \u2013 hydrogen; green- dimethyl ether; red \u2013 carbon monoxide; black \u2013 carbon dioxide; blue \u2013 water; white \u2013 nitrogen; yellow \u2013 argon.<\/em><\/figcaption><\/figure><\/div>\n\n\n\n<p>Also different cycle timings were evaluated experimentally. Overall, material stability has been validated by testing for more than 500 full SEDMES cycles. As shown, the experimental results are in close correlation with the simulated results. Therefore, the model can be used in the future prior to experiments to adjust the process parameters in accordance with a current target.<\/p>\n\n\n\n<div class=\"wp-block-image\"><figure class=\"aligncenter size-large is-resized\"><img loading=\"lazy\" decoding=\"async\" src=\"https:\/\/www.fledged.eu\/wp-content\/uploads\/N6_SEDMESvalidation.png\" alt=\"\" class=\"wp-image-1845\" width=\"373\" height=\"267\" srcset=\"https:\/\/www.fledged.eu\/wp-content\/uploads\/N6_SEDMESvalidation.png 417w, https:\/\/www.fledged.eu\/wp-content\/uploads\/N6_SEDMESvalidation-300x214.png 300w\" sizes=\"auto, (max-width: 373px) 100vw, 373px\" \/><figcaption><em>The model results (solid line) of the adsorption step at 250 \u00b0C vs. experimental results (dashed line)<\/em><\/figcaption><\/figure><\/div>\n\n\n\n<h3 class=\"wp-block-heading\"><strong>Catalyst development for indirect and direct DME synthesis (ICP-CSIC)<\/strong><\/h3>\n\n\n\n<p>The Group of Sustainable Energy and Chemistry from the <em>Instituto de Cat\u00e1lisis y Petroleoqu\u00edmica<\/em>, from CSIC, developed a series of Cu\/ZnO based catalysts for the synthesis of methanol from CO<sub>2<\/sub>-rich bio-syngas and acid catalysts for the production of DME from methanol. The aim was to find the optimal catalyst composition to work under the optimum\u00a0 reaction conditions <em>Sorption Enhanced DME Synthesis<\/em> <em>(SEDMES)<\/em>, performing the reactions with a physical mixture of one of the methanol catalysts and commercial g-Al<sub>2<\/sub>O<sub>3<\/sub> and employing a sorbent zeolite, 3A type. The Cu\/ZnO\/Al<sub>2<\/sub>O<sub>3<\/sub> catalysts were doped with ZrO<sub>2<\/sub> and Ga<sub>2<\/sub>O<sub>3<\/sub> (see Table below). The catalysts were synthesized by coprecipitation of the metallic salts under controlled pH and evaluated in a fixed bed reactor using a syngas with CO<sub>2<\/sub>\/CO-ratio equal to 1.9.<\/p>\n\n\n\n<div class=\"wp-block-image\"><figure class=\"aligncenter size-large is-resized\"><img loading=\"lazy\" decoding=\"async\" src=\"https:\/\/www.fledged.eu\/wp-content\/uploads\/N6_CatalystComparison-1024x773.png\" alt=\"\" class=\"wp-image-1851\" width=\"545\" height=\"411\" srcset=\"https:\/\/www.fledged.eu\/wp-content\/uploads\/N6_CatalystComparison-1024x773.png 1024w, https:\/\/www.fledged.eu\/wp-content\/uploads\/N6_CatalystComparison-300x227.png 300w, https:\/\/www.fledged.eu\/wp-content\/uploads\/N6_CatalystComparison-768x580.png 768w, https:\/\/www.fledged.eu\/wp-content\/uploads\/N6_CatalystComparison-594x449.png 594w, https:\/\/www.fledged.eu\/wp-content\/uploads\/N6_CatalystComparison.png 1026w\" sizes=\"auto, (max-width: 545px) 100vw, 545px\" \/><figcaption>a) CO and CO<sub>2<\/sub> conversion and CH<sub>3<\/sub>\/CO outlet ratio over the catalysts, b) CO outlet concentration.<\/figcaption><\/figure><\/div>\n\n\n\n<ul class=\"wp-block-list\"><li>Both CZA_comm and CZA record the highest CO and CO<sub>2<\/sub> conversions.<\/li><li>Doping the catalysts with ZrO<sub>2<\/sub> decreases CO conversion to ca. 1.6 %, without affecting CO<sub>2<\/sub> conversion.<\/li><li>Ga<sub>2<\/sub>O<sub>3<\/sub> doping (CZAZGa) increases the CO\/CO<sub>2<\/sub> ratio of the syngas (CO conversion of -10.6%)<\/li><li>Negative conversion values indicate that CO is formed during the process via the r-WGS reaction, which is promoted by the addition of ZrO<sub>2<\/sub> and especially Ga<sub>2<\/sub>O<sub>3<\/sub> to CZA.<\/li><\/ul>\n\n\n\n<p>The Direct Synthesis of DME <em>(DDMES) <\/em>form biomass-derived CO<sub>2<\/sub>-rich syngas over a catalytic bed comprising a mixture of the Cu\/ZnO catalysts and g-Al<sub>2<\/sub>O<sub>3<\/sub> was studied at TNO facilities. The effect of <em>in situ <\/em>water removal for the synthesis of DME was also studied under the same conditions using zeolite 3A as water sorbent. This approach is known as <em>Sorption Enhanced DME Synthesis <\/em>(SEDMES). Figure 2 illustrates how experiments were recorded. A catalytic bed containing the Cu\/ZnO catalyst, g-Al<sub>2<\/sub>O<sub>3<\/sub> and zeolite 3A was used. The pre-breakthrough region, when zeolite 3A is capable to remove the H<sub>2<\/sub>O produced, accounts to the SEDMES. After zeolite 3A saturation, the configuration is for the DDMES.<\/p>\n\n\n\n<div class=\"wp-block-image\"><figure class=\"aligncenter size-large is-resized\"><img loading=\"lazy\" decoding=\"async\" src=\"https:\/\/www.fledged.eu\/wp-content\/uploads\/N6_SEDMES_DDMES-1.png\" alt=\"\" class=\"wp-image-1853\" width=\"561\" height=\"266\" srcset=\"https:\/\/www.fledged.eu\/wp-content\/uploads\/N6_SEDMES_DDMES-1.png 864w, https:\/\/www.fledged.eu\/wp-content\/uploads\/N6_SEDMES_DDMES-1-300x142.png 300w, https:\/\/www.fledged.eu\/wp-content\/uploads\/N6_SEDMES_DDMES-1-768x364.png 768w, https:\/\/www.fledged.eu\/wp-content\/uploads\/N6_SEDMES_DDMES-1-594x282.png 594w\" sizes=\"auto, (max-width: 561px) 100vw, 561px\" \/><figcaption>SEDMES and DDMES regimes for the synthesis of DME from CO<sub>2<\/sub>-rich syngas<\/figcaption><\/figure><\/div>\n\n\n\n<div class=\"wp-block-image\"><figure class=\"aligncenter size-large\"><img loading=\"lazy\" decoding=\"async\" width=\"1024\" height=\"378\" src=\"https:\/\/www.fledged.eu\/wp-content\/uploads\/N6_SEDMESconversion-1024x378.png\" alt=\"\" class=\"wp-image-1854\" srcset=\"https:\/\/www.fledged.eu\/wp-content\/uploads\/N6_SEDMESconversion-1024x378.png 1024w, https:\/\/www.fledged.eu\/wp-content\/uploads\/N6_SEDMESconversion-300x111.png 300w, https:\/\/www.fledged.eu\/wp-content\/uploads\/N6_SEDMESconversion-768x283.png 768w, https:\/\/www.fledged.eu\/wp-content\/uploads\/N6_SEDMESconversion-594x219.png 594w, https:\/\/www.fledged.eu\/wp-content\/uploads\/N6_SEDMESconversion.png 1057w\" sizes=\"auto, (max-width: 1024px) 100vw, 1024px\" \/><figcaption>CO and CO<sub>2<\/sub> conversions and DME\/CO outlet ratios for the SEDMES (left panel) and DDMES (right panel) processes<\/figcaption><\/figure><\/div>\n\n\n\n<ul class=\"wp-block-list\"><li>The <em>in situ <\/em>removal of H<sub>2<\/sub>O during the SEDMES process shows a marked effect, displaying higher CO and CO<sub>2<\/sub> conversions than conventional DDMES. <\/li><li>Non promoted CZA catalysts (CZA_comm and CZA) display higher CO<sub>2<\/sub> conversions and DME production than the promoted catalysts in both SEDMES and DDMES regimes. <\/li><li>The effect of ZrO<sub>2<\/sub> and Ga<sub>2<\/sub>O<sub>3<\/sub> doping (CZAZ and CZAZGa), especially Ga<sub>2<\/sub>O<sub>3<\/sub>, is more obvious in the SEDMES process.<\/li><\/ul>\n\n\n\n<div class=\"wp-block-image\"><figure class=\"aligncenter size-large is-resized\"><img loading=\"lazy\" decoding=\"async\" src=\"https:\/\/www.fledged.eu\/wp-content\/uploads\/N6_SEDMESdistribution.png\" alt=\"\" class=\"wp-image-1855\" width=\"565\" height=\"262\" srcset=\"https:\/\/www.fledged.eu\/wp-content\/uploads\/N6_SEDMESdistribution.png 931w, https:\/\/www.fledged.eu\/wp-content\/uploads\/N6_SEDMESdistribution-300x140.png 300w, https:\/\/www.fledged.eu\/wp-content\/uploads\/N6_SEDMESdistribution-768x357.png 768w, https:\/\/www.fledged.eu\/wp-content\/uploads\/N6_SEDMESdistribution-594x276.png 594w\" sizes=\"auto, (max-width: 565px) 100vw, 565px\" \/><figcaption>Products distribution obtained with the DDMES (left panel) and SEDMES (right panel) processes<\/figcaption><\/figure><\/div>\n\n\n\n<p>As clearly shown in Figure 4, H<sub>2<\/sub>O removal during the direct synthesis of DME from CO<sub>2<\/sub>-rich syngas result significantly higher DME production, especially over non-promoted Cu\/ZnO catalysts. However, the actual promotional effect is also affected by the catalyst, thus:<\/p>\n\n\n\n<ul class=\"wp-block-list\"><li>Water removal during SEDMES over CZA catalysts promotes methanol production and dehydration reactions <\/li><li>Water removal during the SEDMES over catalysts with high r-WGS activity promotes CO production<\/li><\/ul>\n\n\n\n<p>In summary, the promotional effect of the SEDMES approach for the direct synthesis of DME from biomass-derived CO<sub>2<\/sub>-rich syngas has been demonstrated experimentally in the frame of FLEDGED project.<\/p>\n\n\n\n<h3 class=\"wp-block-heading\"><strong>2D + 1D heterogeneous dynamic model of the SEDMES synthesis for reactor design and optimization (POLIMI)<\/strong><\/h3>\n\n\n\n<p>The development of the mathematical 2D+1D dynamic model for SEDMES multitubular fixed bed reactor has been completed. The model has been implemented in gPROMS commercial language for the numerical solution and has been validated by a comparison with bench scale reactor experimental data obtained in the TNO facilities in Petten. The model shows the ability to capture the experimental dynamics of the outlet composition of reactants (CO, CO<sub>2<\/sub>) and products (CH<sub>3<\/sub>OH, DME) and also to describe the temperature trajectories in different points along the axial reactor coordinate.<\/p>\n\n\n\n<figure class=\"wp-block-image size-large is-resized\"><img loading=\"lazy\" decoding=\"async\" src=\"https:\/\/www.fledged.eu\/wp-content\/uploads\/N6_ReactorModel.png\" alt=\"\" class=\"wp-image-1857\" width=\"444\" height=\"453\" srcset=\"https:\/\/www.fledged.eu\/wp-content\/uploads\/N6_ReactorModel.png 494w, https:\/\/www.fledged.eu\/wp-content\/uploads\/N6_ReactorModel-294x300.png 294w\" sizes=\"auto, (max-width: 444px) 100vw, 444px\" \/><figcaption>Structure of the mathematical 2D+1D dynamic model for SEDMES multitubular fixed bed reactor.<\/figcaption><\/figure>\n\n\n\n<p>From the local trajectories the envelope of the maximum temperatures along the axial coordinate is obtained. Comparison with the maximum values of temperature measured at the different axial locations during the adsorption\/reaction step shows that the model is able to capture the catalyst temperature stress suffered during SEDMES operation, which is a key parameter in reactor design.<\/p>\n\n\n\n<div class=\"wp-block-image\"><figure class=\"aligncenter size-large\"><img loading=\"lazy\" decoding=\"async\" width=\"1024\" height=\"523\" src=\"https:\/\/www.fledged.eu\/wp-content\/uploads\/N6_ReactorProfiles-1024x523.png\" alt=\"\" class=\"wp-image-1858\" srcset=\"https:\/\/www.fledged.eu\/wp-content\/uploads\/N6_ReactorProfiles-1024x523.png 1024w, https:\/\/www.fledged.eu\/wp-content\/uploads\/N6_ReactorProfiles-300x153.png 300w, https:\/\/www.fledged.eu\/wp-content\/uploads\/N6_ReactorProfiles-768x392.png 768w, https:\/\/www.fledged.eu\/wp-content\/uploads\/N6_ReactorProfiles-594x303.png 594w, https:\/\/www.fledged.eu\/wp-content\/uploads\/N6_ReactorProfiles.png 1059w\" sizes=\"auto, (max-width: 1024px) 100vw, 1024px\" \/><\/figure><\/div>\n\n\n\n<p>The validated model has been used for the analysis and rational design of the industrial scale SEDMES reactor, focusing in particular on the DME yield performances and the thermal management of the exothermic process. The envelope of maximum temperatures achieved along the axial coordinate shows that catalyst thermal stresses in the hotter inlet zone of the reactor slightly increase with the CO content in the with due to faster kinetics of the DME production reactions.<\/p>\n\n\n\n<div class=\"wp-block-image\"><figure class=\"aligncenter size-large is-resized\"><img loading=\"lazy\" decoding=\"async\" src=\"https:\/\/www.fledged.eu\/wp-content\/uploads\/N6_ReactorTmax.png\" alt=\"\" class=\"wp-image-1860\" width=\"273\" height=\"245\" srcset=\"https:\/\/www.fledged.eu\/wp-content\/uploads\/N6_ReactorTmax.png 532w, https:\/\/www.fledged.eu\/wp-content\/uploads\/N6_ReactorTmax-300x269.png 300w\" sizes=\"auto, (max-width: 273px) 100vw, 273px\" \/><\/figure><\/div>\n\n\n\n<p>However, thanks to the dilution effect associated with the large amount of\u00a0 adsorbent material (catalyst:adsorbent=1:4 w\/w), the maximum bed temperature keeps well below the limits reported in the literature (573 K) to preserve the CZA catalyst stability. Accordingly, larger tube diameters (up to 46.6 mm) than in conventional DME direct synthesis reactor can be adopted.<\/p>\n\n\n\n<figure class=\"wp-block-image size-large\"><img loading=\"lazy\" decoding=\"async\" width=\"1024\" height=\"471\" src=\"https:\/\/www.fledged.eu\/wp-content\/uploads\/N6_ReactorAxialProfiles-1024x471.png\" alt=\"\" class=\"wp-image-1859\" srcset=\"https:\/\/www.fledged.eu\/wp-content\/uploads\/N6_ReactorAxialProfiles-1024x471.png 1024w, https:\/\/www.fledged.eu\/wp-content\/uploads\/N6_ReactorAxialProfiles-300x138.png 300w, https:\/\/www.fledged.eu\/wp-content\/uploads\/N6_ReactorAxialProfiles-768x353.png 768w, https:\/\/www.fledged.eu\/wp-content\/uploads\/N6_ReactorAxialProfiles-594x273.png 594w, https:\/\/www.fledged.eu\/wp-content\/uploads\/N6_ReactorAxialProfiles.png 1029w\" sizes=\"auto, (max-width: 1024px) 100vw, 1024px\" \/><\/figure>\n\n\n\n<h3 class=\"wp-block-heading\"><strong>Scientific publications<\/strong><\/h3>\n\n\n\n<p>Several publications on SEDMES and SEG technologies have been released. They are fully accessible from the <a href=\"https:\/\/www.fledged.eu\/download\/scientific-publications\/\" target=\"_blank\" rel=\"noreferrer noopener\">dedicated webpage<\/a>.<\/p>","protected":false},"excerpt":{"rendered":"<p>Newsletter #6 &#8211; September 2020 Download pdf version here. Previous newsletters: Newsletter #1, Newsletter #2, Newsletter #3, Newsletter #4, Newsletter #5 FLEDGED activities on biomass gasification are completed and in the last months the work focused on Sorption-Enhanced DME synthesis \u2026 TRL5 experimental testing of the complete SEDMES operating cycle has been concluded at TNO,&#8230;<\/p>","protected":false},"author":2,"featured_media":731,"parent":122,"menu_order":0,"comment_status":"closed","ping_status":"closed","template":"","meta":{"footnotes":""},"class_list":["post-160","page","type-page","status-publish","has-post-thumbnail","hentry","clearfix","post-index","fader"],"yoast_head":"<!-- This site is optimized with the Yoast SEO plugin v27.3 - https:\/\/yoast.com\/product\/yoast-seo-wordpress\/ -->\n<title>Newsletter - FLEDGED<\/title>\n<meta name=\"robots\" content=\"index, follow, max-snippet:-1, max-image-preview:large, max-video-preview:-1\" \/>\n<link rel=\"canonical\" href=\"https:\/\/www.fledged.eu\/download\/newsletter\/\" \/>\n<meta property=\"og:locale\" content=\"en_US\" \/>\n<meta property=\"og:type\" content=\"article\" \/>\n<meta property=\"og:title\" content=\"Newsletter - FLEDGED\" \/>\n<meta property=\"og:description\" content=\"Newsletter #6 &#8211; September 2020 Download pdf version here. 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